CN213873419U - Nitrogen liquefaction system for parallel production power generation - Google Patents
Nitrogen liquefaction system for parallel production power generation Download PDFInfo
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- CN213873419U CN213873419U CN202022622558.7U CN202022622558U CN213873419U CN 213873419 U CN213873419 U CN 213873419U CN 202022622558 U CN202022622558 U CN 202022622558U CN 213873419 U CN213873419 U CN 213873419U
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/0423—Subcooling of liquid process streams
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a nitrogen gas liquefaction system of parallelly connected product electricity generation, including raw materials nitrogen compressor, main heat exchanger and liquid nitrogen subcooler, there is the circulating nitrogen compressor raw materials nitrogen compressor's output through the pipe connection, the output of circulating nitrogen compressor has connected gradually high temperature expander booster compressor and low temperature expander booster compressor through the pipeline, there is vapour and liquid separator one end of liquid nitrogen subcooler through the pipe connection, vapour and liquid separator's output is connected with liquid expansion machine, the generator is installed to liquid expansion machine's left end, liquid expansion machine's lower extreme has product liquid nitrogen basin through the pipe connection. According to the nitrogen liquefaction system with parallel production power generation and the using method, the refrigeration efficiency of the device is integrally improved by arranging the liquid expansion machine, the production energy is effectively increased, meanwhile, the liquid expansion machine provides kinetic energy to drive the generator to generate power, and the power is newly used for production power utilization.
Description
Technical Field
The utility model relates to a nitrogen liquefaction technical field specifically is a nitrogen liquefaction system of parallelly connected product electricity generation.
Background
The nitrogen liquefaction process in the current market is that low-pressure nitrogen is compressed by a raw material nitrogen compressor, the compressed nitrogen is converged with return gas of a liquefaction device, the compressed nitrogen is divided into two parts after being compressed by a circulating nitrogen compressor, one part of the compressed nitrogen enters a main heat exchanger to be cooled and then is introduced into a high-temperature expansion machine, and the expanded nitrogen is reheated by the main heat exchanger, is discharged out of a cold box and returns to the inlet position of the circulating nitrogen compressor; the other part enters a main heat exchanger after being pressurized by a high-temperature expander and a pressurizing end of a low-temperature expander, is divided into two parts after being cooled, one part is introduced into the low-temperature expander, is reheated by the main heat exchanger after being expanded, and then is discharged out of a cold box and returns to the inlet position of the circulating nitrogen compressor, and the other part is continuously cooled until liquid nitrogen enters a gas-liquid separator after being cooled by a throttling flow; liquid nitrogen pumped by the gas-liquid separator is subcooled in a liquid nitrogen subcooler, throttled and taken as product liquid nitrogen, and enters a product liquid nitrogen storage tank; the problem to be solved at present is how to design a nitrogen liquefaction system with parallel production power and a use method, wherein the nitrogen liquefaction system has good stability, has high refrigeration efficiency through a liquid expansion machine and saves the compression energy consumption of the compressor, and the refrigeration efficiency is low through a throttle valve and the compression energy consumption of the compressor is wasted.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a nitrogen gas liquefaction system of parallelly connected product electricity generation to solve the problem that proposes among the above-mentioned background art.
In order to achieve the above object, the utility model provides a following technical scheme: the utility model provides a parallelly produced nitrogen liquefaction system of electricity generation, includes raw materials nitrogen compressor, main heat exchanger and liquid nitrogen subcooler, the input of raw materials nitrogen compressor is provided with the input port of first nitrogen gas, the output of raw materials nitrogen compressor has the circulating nitrogen compressor through the pipe connection, the output of circulating nitrogen compressor has connected gradually high temperature expander booster compressor and low temperature expander booster compressor through the pipeline to the other end and the input interconnect of high temperature expander, the pipeline that circulating nitrogen compressor and high temperature expander booster compressor are connected is inside to be filled there is third nitrogen gas, the low temperature expander is installed to the right-hand member of low temperature expander booster compressor, the high temperature expander is installed to the right-hand member of high temperature expander booster compressor, the output of low temperature expander booster compressor has the liquid nitrogen subcooler through the pipe connection, the outside one end of liquid nitrogen subcooler is provided with the business turn over pipeline of second liquid nitrogen, the utility model discloses a circulating nitrogen compressor, including liquid nitrogen subcooler, product liquid nitrogen storage tank, main heat exchanger, liquid nitrogen subcooler's one end has gas liquid separator through the pipe connection, gas liquid separator's output is connected with liquid expansion machine, the generator is installed to liquid expansion machine's left end, liquid expansion machine's lower extreme has the product liquid nitrogen storage tank through the pipe connection, main heat exchanger's inside runs through to be provided with respectively in main heat exchanger and follows empty nitrogen gas, from empty dirty ammonia that divides, from empty oxygen and the input port that comes from empty pressure nitrogen that divides, main heat exchanger's inside runs through the delivery outlet that is provided with air behind the heat transfer in main heat exchanger, low temperature expansion machine's lower extreme is connected with the liquid nitrogen and deposits the jar, the intussuseption of liquid nitrogen storage tank is filled with first liquid nitrogen, the upper end that the jar was provided with the pipeline of second nitrogen gas to circulating nitrogen compressor to the second nitrogen gas flows back to the input of circulating nitrogen compressor.
Preferably, the input ends of the low-temperature expander, the high-temperature expander and the product liquid nitrogen storage tank are all provided with control valves, and the control valves are provided with pressure gauges.
Preferably, the output ends of the raw material nitrogen compressor, the circulating nitrogen compressor, the high-temperature expander supercharger, the liquid nitrogen subcooler and the gas-liquid separator are all provided with control valves.
Preferably, the output end, the input end and the pipeline joint of the raw material nitrogen compressor, the circulating nitrogen compressor, the low-temperature expander supercharger, the high-temperature expander supercharger, the liquid nitrogen subcooler, the gas-liquid separator and the product liquid nitrogen storage tank are sealed.
Compared with the prior art, the beneficial effects of the utility model are that: according to the nitrogen liquefaction system with parallel production power generation and the using method thereof, the refrigeration efficiency of the device is integrally improved through the arranged liquid expansion machine, the production energy is effectively increased, meanwhile, the liquid expansion machine provides kinetic energy to drive the generator to generate power, and the power is newly used for production power utilization.
Drawings
Fig. 1 is a schematic view of the overall structure of the present invention.
In the figure: 1. a first nitrogen gas; 2. a raw material nitrogen compressor; 3. a second nitrogen gas; 4. a recycle nitrogen compressor; 5. a third nitrogen gas; 6. a supercharger of a low-temperature expansion machine; 7. a supercharger of a high-temperature expander; 8. a low temperature expander; 9. a high temperature expander; 10. a primary heat exchanger; 11. air after heat exchange; 12. a first liquid nitrogen; 13. a liquid nitrogen subcooler; 14. a second liquid nitrogen; 15. a gas-liquid separator; 16. nitrogen from air separation; 17. ammonia from air separation; 18. oxygen from air separation; 19. from air separation pressure nitrogen; 20. a liquid expander; 21. a generator; 22. and a product liquid nitrogen storage tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "front end", "rear end", "both ends", "one end", "the other end" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element to which the reference is made must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "disposed," "connected," and the like are to be construed broadly, and for example, "connected" may be either fixedly connected or detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Referring to fig. 1, the present invention provides an embodiment: a nitrogen liquefaction system for parallel production power generation comprises a raw material nitrogen compressor 2, a main heat exchanger 10 and a liquid nitrogen subcooler 13, wherein an input port of first nitrogen 1 is arranged at an input end of the raw material nitrogen compressor 2, the first nitrogen 1 is low-pressure nitrogen from air separation, an output end of the raw material nitrogen compressor 2 is connected with a circulating nitrogen compressor 4 through a pipeline, an output end of the circulating nitrogen compressor 4 is sequentially connected with a high-temperature expander supercharger 7 and a low-temperature expander supercharger 6 through pipelines, the other end of the circulating nitrogen compressor is connected with an input end of the high-temperature expander 9, a pipeline connecting the circulating nitrogen compressor 4 and the high-temperature expander supercharger 7 is filled with third nitrogen 5, the third nitrogen 5 is nitrogen compressed by the circulating nitrogen compressor 4, the low-temperature expander 8 is installed at the right end of the low-temperature expander supercharger 6, and the high-temperature expander 9 is installed at the right end of the high-temperature expander supercharger 7, the output end of the booster 6 of the cryogenic expansion machine is connected with a liquid nitrogen subcooler 13 through a pipeline, one end of the outside of the liquid nitrogen subcooler 13 is provided with an inlet and outlet pipeline of second liquid nitrogen 14, the second liquid nitrogen 14 goes to a lower tower, one end of the liquid nitrogen subcooler 13 is connected with a gas-liquid separator 15 through a pipeline, the output end of the gas-liquid separator 15 is connected with a liquid expansion machine 20, the left end of the liquid expansion machine 20 is provided with a generator 21, the lower end of the liquid expansion machine 20 is connected with a product liquid nitrogen storage tank 22 through a pipeline, the inside of the main heat exchanger 10 penetrates through the main heat exchanger 10 and is respectively provided with an inlet for air separation nitrogen 16, air separation waste ammonia 17, air separation oxygen 18 and air separation pressure nitrogen 19, the air separation nitrogen 16, the air separation waste ammonia 17, the air separation oxygen 18 and the air separation pressure nitrogen 19 all go to the main heat exchanger 10, the inside of the main heat exchanger 10 penetrates through the main heat exchanger 10 and is provided with an outlet for heat exchange air 11, the lower extreme of low temperature expander 8 is connected with liquid nitrogen and deposits the jar, and the inside packing that the jar was deposited to liquid nitrogen has first liquid nitrogen 12, and first liquid nitrogen 12 goes to the tower, and the upper end that the jar was deposited to liquid nitrogen is provided with the pipeline of second nitrogen 3 to 3 refluxes of second nitrogen to the input of circulating nitrogen compressor 4, and second nitrogen 3 is the inflation nitrogen gas that flows backwards.
Further, the input ends of the low-temperature expander 8, the high-temperature expander 9 and the product liquid nitrogen storage tank 22 are all provided with control valves, and pressure gauges are installed on the control valves.
Further, the output ends of the raw material nitrogen compressor 2, the circulating nitrogen compressor 4, the high temperature expander supercharger 7, the liquid nitrogen subcooler 13 and the gas-liquid separator 15 are all provided with control valves.
Further, the output end, the input end and the pipeline connection of the raw material nitrogen compressor 2, the circulating nitrogen compressor 4, the low temperature expander supercharger 6, the high temperature expander supercharger 7, the liquid nitrogen subcooler 13, the gas-liquid separator 15 and the product liquid nitrogen storage tank 22 are all sealed.
The utility model discloses a still provide the application method that can accurate guide river lake deposit column sampling device:
when the first nitrogen gas 1 is compressed by a raw material nitrogen compressor 2, is merged with the second nitrogen gas 3 of a liquefying device after being compressed by a circulating nitrogen compressor 4, is divided into two parts, one part enters a main heat exchanger 10 for cooling and then is introduced into a high-temperature expander 9, is reheated by the main heat exchanger 10 after being expanded and returns to the inlet position of the circulating nitrogen compressor 4, the other part enters the main heat exchanger 10 after being pressurized by a low-temperature expander supercharger 6 and a high-temperature expander supercharger 7, is divided into two parts after being cooled, one part is introduced into a low-temperature expander 8, is reheated by the main heat exchanger 10 after being expanded and returns to the inlet position of the circulating nitrogen compressor 4, the other part is continuously cooled until liquid nitrogen is extracted and enters a liquid expander 20 after being expanded, enters a gas-liquid separator 15, and is subcooled in a liquid nitrogen subcooler 13 through the gas-liquid separator 15 and then is throttled to be used as a product liquid nitrogen, into product liquid nitrogen storage 22.
It is obvious to a person skilled in the art that the invention is not restricted to details of the above-described exemplary embodiments, but that it can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (4)
1. The utility model provides a nitrogen gas liquefaction system of parallelly connected product electricity generation, includes raw materials nitrogen compressor (2), main heat exchanger (10) and liquid nitrogen subcooler (13), its characterized in that: the input of raw materials nitrogen compressor (2) is provided with the input port of first nitrogen gas (1), there is circulating nitrogen compressor (4) the output of raw materials nitrogen compressor (2) through the pipe connection, the output of circulating nitrogen compressor (4) has connected gradually high temperature expander booster compressor (7) and low temperature expander booster compressor (6) through the pipeline to the input interconnect of the other end and high temperature expander (9), the pipeline that circulating nitrogen compressor (4) and high temperature expander booster compressor (7) are connected is inside to be filled with third nitrogen gas (5), low temperature expander (8) are installed to the right-hand member of low temperature expander booster compressor (6), high temperature expander (9) are installed to the right-hand member of high temperature expander booster compressor (7), the output of low temperature expander booster compressor (6) has liquid nitrogen subcooler (13) through the pipe connection, the utility model discloses a heat exchanger, including liquid nitrogen subcooler (13), the outside one end of liquid nitrogen subcooler (13) is provided with the business turn over pipeline of second liquid nitrogen (14), the one end of liquid nitrogen subcooler (13) has vapour and liquid separator (15) through the pipe connection, the output of vapour and liquid separator (15) is connected with liquid expander (20), generator (21) are installed to the left end of liquid expander (20), the lower extreme of liquid expander (20) has product liquid nitrogen storage tank (22) through the pipe connection, the inside of main heat exchanger (10) is run through and is provided with respectively in main heat exchanger (10) and is come from empty nitrogen gas (16), come from empty dirty ammonia (17), come from empty oxygen (18) and come from the input port of empty pressure nitrogen (19) that divides, the inside of main heat exchanger (10) is run through and is provided with the delivery outlet of heat transfer back air (11) in main heat exchanger (10), the lower extreme of low temperature expander (8) is connected with the liquid nitrogen and deposits the jar, the inside packing of jar is deposited to liquid nitrogen has first liquid nitrogen (12), the upper end of jar is deposited to liquid nitrogen is provided with the pipeline of second nitrogen gas (3) to second nitrogen gas (3) flow back to the input of circulating nitrogen compressor (4).
2. The nitrogen liquefaction system with cogeneration of claim 1, wherein: the input ends of the low-temperature expander (8), the high-temperature expander (9) and the product liquid nitrogen storage tank (22) are all provided with control valves, and pressure gauges are installed on the control valves.
3. The nitrogen liquefaction system with cogeneration of claim 1, wherein: and the output ends of the raw material nitrogen compressor (2), the circulating nitrogen compressor (4), the high-temperature expander supercharger (7), the liquid nitrogen subcooler (13) and the gas-liquid separator (15) are all provided with control valves.
4. The nitrogen liquefaction system with cogeneration of claim 1, wherein: the output end, the input end and the pipeline joint of the raw material nitrogen compressor (2), the circulating nitrogen compressor (4), the low-temperature expander supercharger (6), the high-temperature expander supercharger (7), the liquid nitrogen subcooler (13), the gas-liquid separator (15) and the product liquid nitrogen storage tank (22) are all sealed.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022622558.7U CN213873419U (en) | 2020-11-13 | 2020-11-13 | Nitrogen liquefaction system for parallel production power generation |
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| CN202022622558.7U CN213873419U (en) | 2020-11-13 | 2020-11-13 | Nitrogen liquefaction system for parallel production power generation |
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| CN213873419U true CN213873419U (en) | 2021-08-03 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114234556A (en) * | 2022-02-24 | 2022-03-25 | 杭州制氧机集团股份有限公司 | Boosting and vaporizing device for recycling liquid oxygen cold and using method thereof |
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2020
- 2020-11-13 CN CN202022622558.7U patent/CN213873419U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114234556A (en) * | 2022-02-24 | 2022-03-25 | 杭州制氧机集团股份有限公司 | Boosting and vaporizing device for recycling liquid oxygen cold and using method thereof |
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Address after: 317000 No. 755, Dongdu South Road, Linhai City, Taizhou City, Zhejiang Province (for office use only) (self declaration) Patentee after: Zhejiang Haichang Gas Co.,Ltd. Address before: 317000 southeast of line A3, Linhai chemical API base, Linhai Park, Taizhou City, Zhejiang Province Patentee before: ZHEJIANG HAICHANG GAS Co.,Ltd. |
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